Process for recycling a cobalt hydroformylation catalyst

ABSTRACT

An improved process for recycling a cobalt hydroformylation catalyst from a hydroformylation reaction which comprises feeding a hydroformylation product into a separation zone wherein two phases are formed, a solvent phase containing the cobalt hydroformylation catalyst and another phase containing the catalyst and a hydroformylation compound; separating the catalyst from the hydroformylation compound in a countercurrent extractor; concentrating the catalyst in an evaporation zone and recycling it into the hydroformylation reaction.

United States Patent [1 1 Aycock et a1.

[ PROCESS FOR RECYCLING A COBALT HYDROFORMYLATION CATALYST [75] Inventors: David F. Aycock, Lenox; Daniel E.

Sliva, Pitt'sfield, both of Mass.

[73] Assignee: General Electric Company,

Pittsfield, Mass.

[22] Filed: June 6, 1973 [21] Appl. No.: 367,551

[52] 11.8. C1 252/414; 260/429 R; 260/439 R, 260/638 HF [51] Int. Cl.' .4 BOlD 15/06; 801.1 37/00 [58] Field of Search 252/414; 260/638 HF, 429 R, 260/439 R; 423/139 4 1 Sept. 9, 1975 3,622,499 11/1971 Stine ct a1 v. 252/414 3,634,291 1/1972 Usami et a1 252/414 3,772,211 11/1973 Mounce 252/414 [57] ABSTRACT An improved process for recycling a cobalt hydrofor mylation catalyst from a hydroformylation reaction which comprises feeding a hydroformylation product into a separation zone wherein two phases are formed, a solvent phase containing the cobalt hydroformylation catalyst and another phase containing the catalyst and a hydroformylation compound; separating the catalyst from the hydroformylation compound in a countercurrent extractor; concentrating the catalyst in an evaporation zone and recycling it into the hydroformylation reaction.

9 Claims, No Drawings PROCESS FOR RECYCLING A COBALT HYDROFORMYLATION CATALYST BACKGROUND OF THE INVENTION It is known that the hydroformylation of olefins takes place in the presence of a soluble catalyst. The metal catalyst, usually cobalt, is converted to carbonyls under synthesis conditions and leaves the reaction chamber in this form, dissolved in the reaction products.

The mobility of the catalyst makes it necessary to remove the dissolved cobalt from the reaction products (decobaltation) and then to restore the recovered cobalt to the initial form under which it was introduced into the reaction chamber (regeneration). The method of decobaltation and regeneration is generally called catalyst recycle.

Several methods of decobalting and regenerating the catalyst are known in the prior art. Among these methods are decomposing a cobalt carbonyl in the reactor product by heat and/or aqueous acids, adding aqueous solutions of cobaltous ions to remove the cobalt carbonyl from the organic phase by formation of a cobalt salt and decobalting with an aqueous alkali at high pressures and temperatures to form the alkali metal salt of cobalt hydroearbonyl. All of these methods have the fundamental defect of destroying the catalyst either completely or partially after the synthesis. This requires reconstitution of the catalyst from the recovered cobalt by passing through intermediate cobalt compounds.

DESCRIPTION OF THE INVENTION It has been discovered that the cobalt hydroformylation catalyst may be recycled in the same form that it is used in the hydroformylation reaction, i.e., active form, without destroying the catalyst.

The instant invention is concerned with an improved process for recycling a cobalt hydroformylation catalyst from a hydroformylation reaction wherein an olefinic compound is reacted with carbon monoxide and hydrogen in the presence ofa cobalt hydroformylation catalyst dissolved in an organic solvent in a reaction zone under hydroformylation conditions to produce a hydroformylation product comprising a hydroformylation compound and the cobalt hydroformylation catalyst, wherein the improvement comprises the steps of: (a) feeding the hydroformylation product into a separation Zone wherein two phases are formed, an upper or solvent phase containing the cobalt hydroformyla tion catalyst and a lower phase containing the cobalt hydroformylation catalyst and the hydroformylation compound; (b) then separating the lower phase therefrom and feeding it into a countercurrent extractor with an organic solvent to remove the cobalt hydroformylation catalyst therefrom; (c) then passing the upper or solvent phase from the separation zone and the cobalt hydroformylation catalyst from the countercurrent extractor into an evaporation zone to remove solvent therefrom to form a concentrated solution of the cobalt hydroformylation catalyst; (d) then recycling the concentrated cobalt hydroformylation catalyst into thoinitial reaction zone.

The term hydroformylation compound includes an aldehyde or its isomeric products, an alcohol or its isomeric products or mixtures thereof.

The hydroformylation process is known in the art and it involves reacting an olefinic compound with carbon monoxide and hydrogen at an elevated temperature and pressure in the presence of a hydroformylation catalyst to produce a hydroformylation compound comprising an aldehyde or its isomeric products, an alcohol or its isomeric products or mixtures thereof.

The olefinic compounds to be hydroformylated are those which can be hydroformlated to produce a hydroformylation compound comprising an aldehyde or its isomeric products, an alcohol or its isomeric products or mixtures thereof, which hydroformylation product is soluble in water and essentially insoluble in the organic solvent employed. These olefinic compounds are known in the art and include compounds such as any aliphatic or cycloaliphatic compounds having at least one aliphatic carbon-to-carbon unsaturation, especially an ethylenic carbon-to-carbon bond. Also included are substituted olefins such as ethers, esters, aldehydes, alcohols, etc., containing olefinic unsaturation. Thus, the process may be applied to the hydroformylation of any olefinic compound which produces compounds comprising an aldehyde or its isomeric products, an alcohol or its isomeric products or mix tures thereof soluble in water and essentially insoluble in the organic solvent employed and having one more carbon atom than the starting olefinic compound. A preferred olefinic compound is an ester such as allyl acetate.

The hydroformylation is carried out under hydroformylation conditions which are temperatures and pressures known to those skilled in the art. Preferably, pressures of from about i000 to about 5000 psi and temperatures in the range of from about to about 200C. are employed. Somewhat higher or lower temperatures and pressures may, however, be employed within the scope of this invention.

The ratios of hydrogen to carbon monoxide of the synthesis gas (carbon monoxide and hydrogen) charged may vary widely within limits known to those skilled in the art. Suitable ratios of hydrogen to carbon monoxide comprise those within the ratio of from about 1:3 to about l():l. Higher or lower ratios, how ever, are within the limits of the art skilled.

The cobalt hydroformylation catalyst employed in the instant invention may be complexed cobalt. The complexed cobalt may be cobalt in complex combination with carbon monoxide. A preferred cobalt catalyst in complex combination with carbon monoxide is dicobalt octacarbonyl. The active form of this catalyst is a cobalt hydroearbonyl which results from cleavage of the dicobalt octacarbonyl.

Also included within the scope of this invention are modified complexed cobalt catalysts. The complexed cobalt catalysts may be modified by the inclusion of, for example. phosphorus-containing or arseniccontaining ligands in the molecule. Preferably, alkyl, aryl and heterocyclic phosphines are employed. These phosphine modified complexed cobalt catalysts are prepared in accordance with the methods described in U.S. Pat. Nos. 3,239,569; 3,420,898 and 3,496,203, for example.

The active form of the catalyst can be prepared by any of the methods used in the prior art. For example, the various metal salts, the metal powder or metal oxide can be reacted with carbon monoxide and hydrogen to form the carbonyl which can then be converted to the hydroearbonyl by further hydrogenation. Actu ally, these reactions can be carried out right in the reac tor in which the hydroformylation reaction is to be carried out since the metal. its salts or its carbonyl. either prior to or upon establishing the hydroformylating conditions to be used. will be converted into the hydrocarbonyl. In order to hasten this reaction. it is preferable to use cobalt compounds which are soluble in the reaction mixture, for example, the carbonyl salts of carboxylic acids. Therefore. it is preferred in using cobalt as the hydroformylation catalyst. to introduce it into the reaction mixture in the form of its carbonyl or a salt soluble in the reaction mixture. No matter what form the cobalt is added to the reaction. its active catalytic form is believed to be cobalt hydrocarbonyl. also called cobalt tetracarbonyl hydride.

The form of cobalt present in the hydroformylation reaction mixture is a function of the operating conditions. Not only are different forms produced in the carbonyl formation reaction itself. but also equilibria exist between various carbonyls and between the carbonyls and the metal which are governed by reaction variables such as temperature, carbon monoxide pressure. hy-

drogen pressure. liquid-phase cobalt concentration. etc. Because of this variable nature of the cobalt catalyst in the reaction mixture the various forms are best described as cobalt hydroformylation catalysts.

The hydroformylation reaction is generally carried out in conventional pressure vessels. such as tanks, towers, autoclaves, or tubular reactors, particularly designed to maintain necessary pressures and temperatures of the reaction.

There are a number of ways in which the hydroformylation reaction may be carried out. Among these processes are those in which the reaction is started at relatively low temperatures. which produces primarily an aldehyde or its isomeric products. The reaction may be then heated to higher temperatures which produce primarily an alcohol or its isomeric products. Alternativcly. the whole process may be carried out at the higher temperature wherein primarily an alcohol or its isomeric products is produced. However. at low temperaturcs, the aldehyde product may contain some alcohol and at high temperatures the alcohol may contain some aldehyde.

ln hydroformylating allyl acetate. if the reaction is carried out at temperatures of l l 50C.. the following hydroformylation compounds are produced in admixture: 4-acctoxybutyraldehyde. 2-mcthyl-3-acetoxy propionaldehyde and 2acctoxybutyraldchyde. If the reaction is then heated to temperatures of up to 180C. or higher. or if the reaction is carried out starting at the higher temperature. the following hydroformylation compounds are produced in admixture: 4- acetoxybutanol; 1.4-butanediol; l,4-butanediol diacclate; 2mcthyl-3-acetoxypropanol; 2mcthyll .3- propancdiol; 2methyli .3propancdiol diacctatc; 2- acetoxybutanol; LZ-butancdiol and l.2-butanediol diacetate.

The organic solvent which is employed in the instant invention may be any solvent in which the aldehyde or its isomeric products or the alcohol or its isomeric products or the mixture thereof produced from the hy droformylation reaction is essentially insoluble. A pre fcrrcd organic solvent is an aliphatic hydrocarbon such as heptane, kerosene. n-dccanc. etc.

The instant catalyst recycle comprises continuously removing the hydroformylation product from the initial reaction zone where hydroformylation takes place and feeding it into a separation zone. Two phases are formed in the separation zone. an upper or solvent phase containing the cobalt hydroforrnylation catalyst and a lower phase containing the cobalt hydroformylation catalyst and a hydroformylation product. Both the upper and lower phase contain the active cobalt hydroformylation catalyst. with the upper phase containing a greater proportion of said catalyst. The hydroformylation product in the lower phase is an aldehyde or its isomeric product, an alcohol or its isomeric product. or mixtures thereof.

The lower phase is separated and fed into a countercurrent extractor. Solvent is added to the countercurrent extractor which removes the active cobalt hydroformylation catalyst from the phase containing both the catalyst and the hydroformylation compound. The active cobalt hydroformylation catalyst is then fed from the countercurrent extractor into an evaporation zone. The hydroformylation compound which is dissolved in solvent is removed from the countercurrent extractor.

The upper or solvent phase from the separation zone is fed together with the active cobalt hydroformylation catalyst from the countercurrent extractor into an evaporation zone where solvent is removed to concentrate the active cobalt hydroformylation catalyst to the same concentration as the catalyst going into the hydroformylation reaction. The active cobalt hydroformylation catalyst is recycled from the evaporation zone into the initial reaction zone. The solvent which is removed in the evaporation zone may be recycled back into the countercurrent extractor where it is used to remove the active cobalt hydroformylation catalyst from the phase containing both the catalyst and the hydroformylation compound.

The instant catalyst recycle may be carried out in batch, semi-continuously, or continuously. Preferably. the catalyst recycle is carried out continuously.

The separation is carried out in conventional vessels. such as tanks. towers or pressure tanks or towers. while the evaporation is carried out in conventional distilling apparatus. The countercurrent extractor that is used is well known in the art.

The catalyst recycle may be carried out at a temperature of from about room temperature to about C. and pressures from sub-atmospheric to elevated pressure. Preferably. the separation and evaporation vessels and the countercurrent extractor are under a carbon monoxide pressure of about one atmosphere. The carhon monoxide atmosphere aids in preventing any de composition of the cobalt hydroformylation catalyst.

DESCRIPTION OF THE PREFERRED EMBODIMENT The following Examples are set forth to illustrate more clearly the principle and practice of this invention to those skilled in the art. Unless otherwise specified. where parts or percents are mentioned. they are parts or percents by weight.

EXAMPLE l Allyl acetate and a heptanc solution of cobalt carbonyls (3.5 g./liter as cobalt) are pumped separately. at equal rates. into a l liter stirred autoclave. The autoclave is heated to l50C. and is pressurized to 3000 psi with an equal volume gas mixture of hydrogen and carbon monoxide. The product is continuously removed from the autoclave and added to a settling chamber where the heptanc layer and the aldehyde layer are separated. The heptane layer contains 55% of the cobalt carbonyl catalyst and the aldehyde layer contains 45% of the catalyst. The aldehyde layer is passed through a continuous countereurrent extractor where all of the cobalt catalyst is removed by heptane. Heptane is distilled at 40C. under reduced pressure to concentrate the catalyst. This concentrated catalyst is recycled back to the autoclave.

EXAMPLE 2 Allyl acetate and a pentane solution of cobalt carbonyls (3.5 g/liter as cobalt) are pumped separately. at equal rates, into a 1 liter stirred autoclave. The autoclave is heated to 150C. and is pressurized to 3000 psi with an equal volume gas mixture of hydrogen and carbon monoxide. A stream is continuously pumped from the autoclave into a settling chamber where two phases are formed. The upper pentane phase contains about 55% of the cobalt carbonyl catalyst and the lower phase contains the aldehyde 'isoiner products'of allyl acetate along with about 45% of the cobalt carbonyl catalyst. The lower phase is passed through a continuous countereurrent extractor, where pentane is used to remove the cobalt carbonyl catalyst. The pentane phase from the settling chamber and the countereurrent extractor are sent to an evaporator to concentrate the cobalt carbonyl catalyst to the concentration of the catalyst stream being pumped into the autoclave. The evaporated pentane is recycled to the continuous countereurrent extractor. The concentrated catalyst solution is recycled back to the autoclave.

EXAMPLE 3 l l3.0 g. of allyl acetate. 6.0 g. of cobalt acetate and 300 ml. of pentane are placed in a 1 liter autoclave and pressurized to 3000 psi with an equal volume gas mixture of hydrogen and carbon monoxide. The autoclave is heated to 145C. where an exotherm starts which raises the temperature of the autoclave to 250C. The temperature is maintained at about 190C. for l hour. After cooling, the mixture from the autoclave is found to contain two layers. The bottom layer, containing the alcohol products of allyl acetate and some cobalt carbonyl catalyst is extracted with 4 equal volume portions of pentane to remove the catalyst. The pentane used for the extractions and the top layer of pentane from the autoclave are combined and 400 ml. of pentane are distilled to obtain a catalyst concentration equal to that initially used to charge the reactor. The concentrated catalyst solution is added together with l l 3.0 g. of allyl acetate to the autoclave and the above procedure is repeated.

It should, of course. be apparent to those skilled in the art that changes may be made in the particular embodiments of the invention described which are within the full intended scope of the invention as defined by the appended claims.

What is claimed is:

1. In an improved process for recycling a cobalt hydroformylation catalyst from a hydroformylation reaction wherein an olcfinic compound is reacted with carbon monoxide and hydrogen in the presence ofa cobalt hydroformylation catalyst dissolved in an inert organic solvent in a reaction zone under hydroformylation conditions to produce a hydroformylation product comprising a hydroformylation compound and the cobalt hydroformylation catalyst, wherein the improvement comprises the steps of:

a. feeding the hydroformylation product into a separation zone wherein two phases are formed, an upper or solvent phase containing the cobalt hydroformylation catalyst and a lower phase containing the cobalt hydroformylation catalyst and the hydroformylation compound;

b. then separating the lower phase therefrom and feeding it into a countereurrent extractor with an inert organic solvent to remove the cobalt hydroformylation catalyst therefrom;

c. then passing the upper or solvent phase from the separation zone and the cobalt hydroformylation catalyst from the countereurrent extractor into an evaporation zone to remove solvent therefrom to form a concentrated solution of the cobalt hydroformylation catalyst;

d. then recycling the concentrated cobalt hydroformylation catalyst into the initial reaction zone."

2. The process of claim 1 wherein the hydroformylation product comprises in admixture an aldehyde or its isomeric products, an alcohol or its isomeric products or mixtures thereof.

3. The process of claim 1 wherein the organic solvent is an aliphatic hydrocarbon.

4. The process of claim 1 wherein the olefinic compound is allyl acetate.

5. The process of claim 1 wherein the cobalt hydroformylation catalyst is dicobalt octacarbonyl.

6. The process of claim 1 wherein the hydroformylation is carried out at a temperature of from about to about 200C.

7. The process of claim 1 wherein the hydroformylation is carried out at pressures from about i000 to about 5000 psi.

8. In an improved process for recycling a cobalt hydroformylation catalyst from a hydroformylation reaction wherein allyl acetate is reacted with carbon monoxide and hydrogen in the presence of a cobalt hydroformylation catalyst dissolved in an inert organic solvent in a reaction zone under hydroformylation conditions to produce a hydroformylation product comprising, in admixture, hydroformylation compounds consisting of 4-acetoxybutyraldehyde, 2-methyl-3- acetoxypropionaldehyde and Z-acetoxy-butyraldehyde and the cobalt hydroformylation catalyst, wherein the improvement comprises the steps of:

a. feeding the hydroformylation product into a separation zone wherein two phases are formed, an upper or solvent phase containing the cobalt hydroformylation catalyst and a lower phase containing the cobalt hydroformylation catalyst and the hydroformylation compound;

b. then separating the lower phase therefrom and feeding it into a countereurrent extractor with an inert organic solvent to remove the cobalt hydroformylation catalyst therefrom;

c. then passing the upper or solvent phase from the separation zone and the cobalt hydroformylation catalyst from the countereurrent extractor into an evaporation zone to remove solvent therefrom to form a concentrated solution of the cobalt hydroformylation catalyst;

d. then recycling the concentrated cobalt hydrofor mylation catalyst into the initial reaction zone.

wrvpnv r mar 9. In an improved process for recycling a cobalt hydroformylation catalyst from a hydroformylation reaction wherein an olefinic compound is reacted with carbon monoxide and hydrogen in the presence of a cobalt hydroformylation catalyst dissolved in an inert organic solvent in a reaction zone under hydroformylation conditions to produce a hydroformylation product comprising in admixture: a hydroformylation compound consisting of 4-acetoxybutanol; lA-butanediol; l 4 butanediol diacetate; 2-methyl-3-acetoxypropanol; 2-methyll 3-propanediol; Zmethyl-l 3-propanediol diaeetate; 2-acetoxybutanol; l,2-butanediol; l,2- butanediol diacetate and the cobalt hydroformylation catalyst, wherein the improvement comprises the steps of:

a. feeding the hydroformylation product into a separation zone wherein two phases are formed, an

upper or solvent phase containing the cobalt hydroformylation catalyst and a lower phase containing the cobalt hydroformylation catalyst and the hydroformylation compound;

b. then separating the lower phase therefrom and feeding it into a countercurrent extractor with an inert organic solvent to remove the cobalt hydroformylation catalyst therefrom;

. then passing the upper or solvent phase from the d. then recycling the concentrated cobalt hydrofor mylation catalyst into the initial reaction zone. 

1. IN AN IMPROVED PROCESS FOR RECYCLING A COBALT HYDROFORMYTATION CATALYST FROM A HYDROFORMYLATION REACTION WHEREIN AN OLEFINIC COMPOUND IS REACTED WITH CARBON MONOXIDE AND HYDROGEN IN THE PRESENCE OF A COBALT HYDROFORMYLATION CATALYST DISSOLVED IN AN INERT ORGANIC SOLVENT IN A REACTION ZONE UNDER HYDROFORMYLATION CONDITIONS TO PRODUCE A HYDROFORMYLATION PRODUCT COMPRISING A HYDROFORMYLATION COMPOUND AND THE COBALT HYDROFORMYLATION CATALYST, WHEREIN THE IMPROVEMENT COMPRISES THE STEPS OF: A. FEEDING THE HYDROFORMYLATION PRODUCT INTO A SEPARATION ZONE WHEREIN TWO PHASES ARE FORMED, AN UPPER OR SOLVENT PHASE CONTAINING THE COBALT HYDROFORMYLATION CATALYST AND A LOWER PHASE CONTAINING THE COBALT HYDROFORMYLATION CATALYST AND THE HYDROFORMYLATION COMPOUND, B. THEN SEPARATING THE LOWER PHASE THEREFROM AND FEEDING IT INTO A COUNTERCURRENT EXTRACTOR WITH AN INERT ORGANIC SOLVENT TO REMOVE THE COBALT HYDROFORMYLATION CATALYST THEREFROM, C. THEN PASSING THE UPPER OR SOLVENT PHASE FROM THE SEPARATION ZONE AND THE COBALT HYDROFORMYLATION CATALYST FROM THE COUNTERCURRENT EXTRACTOR INTO AN EVAPORATION ZONE TO REMOVE SOLVENT THEREFROM TO FORM A CONCENTRATED SOLUTION OF THE COBALT HYDROFORMYLATION CATALYST, D. THEN RECYCLONG THE CONCENTRATED COBALT HYDROFORMYLATION CATALYST INTO THE INITIAL REACTION ZONE.
 2. The process of claim 1 wherein the hydroformylation product comprises in admixture an aldehyde or its isomeric products, an alcohol or its isomeric products or mixtures thereof.
 3. The process of claim 1 wherein the organic solvent is an aliphatic hydrocarbon.
 4. The process of claim 1 wherein the olefinic compound is allyl acetate.
 5. The process of claim 1 wherein the cobalt hydroformylation catalyst is dicobalt octacarbonyl.
 6. The process of claim 1 wherein the hydroformylation is carried out at a temperature of from about 100* to about 200* C.
 7. The process of claim 1 wherein the hydroformylation is carried out at pressures from about 1000 to about 5000 psi.
 8. In an improved process for recycling a cobalt hydroformylation catalyst from a hydroformylation reaction wherein allyl acetate is reacted with carbon monoxide and hydrogen in the presence of a cobalt hydroformylation catalyst dissolved in an inert organic solvent in a reaction zone under hydroformylation conditions to produce a hydroformylation product comprising, in admixture, hydroformylation compounds consisting of 4-acetoxybutyraldehyde, 2-methyl-3-acetoxypropionaldehyde and 2-acetoxy-butyraldehyde and the cobalt hydroformylation catalyst, wherein the improvement comprises the steps of: a. feeding the hydroformylation product into a separation zone wherein two phases are formed, an upper or solvent phase containing the cobalt hydroformylation catalyst and a lower phase containing the cobalt hydroformylation catalyst and the hydroformylation compound; b. then separating the lower phase therefrom and feeding it into a countercurrent extractor with an inert organic solvent to remove the cobalt hydroformylation catalyst therefrom; c. then passing the upper or solvent phase from the separation zone and the cobalt hydroformylation catalyst from the countercurrent extractor into an evaporation zone to remove solvent therefrom to form a concentrated solution of the cobalt hydroformylation catalyst; d. then recycling the concentrated cobalt hydroformylation catalyst into the initial reaction zone.
 9. In an improved process for recycling a cobalt hydroformylation catalyst from a hydroformylation reaction wherein an olefinic compound is reacted with carbon monoxide and hydrogen in the presence of a cobalt hydroformylation catalyst dissolved in an inert organic solvent in a reaction zone under hydroformylation conditions to produce a hydroformylation product comprising in admixture: a hydroformylation compound consisting of 4-acetoxybutanol; 1,4-butanediol; 1,4-butanediol diacetate; 2-methyl-3-acetoxypropanol; 2-methyl-1,3-propanediol; 2methyl-1,3-propanediol diacetate; 2-acetoxybutanol; 1,2-butanediol; 1,2-butanediol diacetate and the cobalt hydroformylation catalyst, wherein the improvement comprises the steps of: a. feeding the hydroformylation product into a separation zone wherein two phases are formed, an upper or solvent phase containing the cobalt hydroformylation catalyst and a lower phase containing the cobalt hydroformylation catalyst and the hydroformylation compound; b. then separating the lower phase therefrom and feeding it into a countercurrent extractor with an inert organic solvent to remove the cobalt hydroformylation catalyst therefrom; c. then passing the upper or solvent phase from the separation zone and the cobalt hydroformylation catalyst from the countercurrent extractor into an evaporation zone to remove solvent therefrom to form a concentrated solution of the cobalt hydroformylation catalyst; d. then recycling the concentrated cobalt hydroformylation catalyst into the initial reaction zone. 